RU2018109132A - IMPROVED DESIGN OF OLIGOMERIZATION / TRIMERIZATION / ETHYLENE TETRAMERIZATION REACTOR - Google Patents

IMPROVED DESIGN OF OLIGOMERIZATION / TRIMERIZATION / ETHYLENE TETRAMERIZATION REACTOR Download PDF

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RU2018109132A
RU2018109132A RU2018109132A RU2018109132A RU2018109132A RU 2018109132 A RU2018109132 A RU 2018109132A RU 2018109132 A RU2018109132 A RU 2018109132A RU 2018109132 A RU2018109132 A RU 2018109132A RU 2018109132 A RU2018109132 A RU 2018109132A
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reaction system
reaction mixture
reaction
heat exchange
heat
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RU2018109132A
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Russian (ru)
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RU2018109132A3 (en
RU2738407C2 (en
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Брюс КРЕЙШЕР
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ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи
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Priority claimed from US14/858,526 external-priority patent/US10519077B2/en
Priority claimed from US14/858,588 external-priority patent/US10513473B2/en
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    • B01J19/0013—Controlling the temperature of the process
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    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
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    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
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    • B01J2219/0072—Organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
    • B01J2231/20—Olefin oligomerisation or telomerisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
    • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
    • B01J2531/84—Metals of the iron group
    • B01J2531/847—Nickel

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Claims (55)

1. Способ, включающий:1. The method comprising: периодическое или непрерывное введение олефинового мономера, и периодическое или непрерывное введение каталитической системы или компонентов каталитической системы в реакционную смесь реакционной системы;periodically or continuously introducing the olefin monomer, and periodically or continuously introducing the catalyst system or components of the catalyst system into the reaction mixture of the reaction system; олигомеризацию олефинового мономера в реакционной смеси с образованием олигомерного продукта; иoligomerizing the olefin monomer in the reaction mixture to form an oligomeric product; and периодический или непрерывный вывод выходящего потока реакционной системы, содержащего олигомерный продукт, из реакционной системы,periodic or continuous withdrawal of the effluent of the reaction system containing the oligomeric product from the reaction system, причем реакционная система содержит общий объем реакционной смеси реакционной системы; и теплообменный участок реакционной системы, содержащий объем теплообменной реакционной смеси и общую площадь поверхности теплообмена, обеспечивающую непрямой термоконтакт между реакционной смесью и теплоносителем;moreover, the reaction system contains the total volume of the reaction mixture of the reaction system; and a heat exchange portion of the reaction system containing a volume of the heat exchange reaction mixture and a total heat exchange surface area providing indirect thermal contact between the reaction mixture and the heat carrier; при этом соотношение общей площади теплообменной поверхности к общему объему реакционной смеси реакционной системы находится в диапазоне от 0,75 дюйм-1 до 5 дюйм-1; иthe ratio of the total area of the heat exchange surface to the total volume of the reaction mixture of the reaction system is in the range from 0.75 inch -1 to 5 inch -1 ; and при том, что скорость вывода олигомерного продукта из реакционной системы составляет между от 1,0 (фунт)(час-1)(галлон-1) до 6,0 (фунт)(час-1)(галлон-1).while the rate of withdrawal of the oligomeric product from the reaction system is between 1.0 (lb) (hour -1 ) (gallon -1 ) to 6.0 (lb) (hour -1 ) (gallon -1 ). 2. Способ по п. 1, дополнительно включающий периодическое или непрерывное введение реакционного растворителя в реакционную смесь реакционной системы.2. The method of claim 1, further comprising periodically or continuously introducing the reaction solvent into the reaction mixture of the reaction system. 3. Способ по п. 1, отличающийся тем, что соотношение общей площади теплообменной поверхности реакционной системы к общему объему реакционной смеси реакционной системы находится в диапазоне от минимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)]-1,16 до максимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)] + 0,76.3. The method according to p. 1, characterized in that the ratio of the total area of the heat exchange surface of the reaction system to the total volume of the reaction mixture of the reaction system is in the range from the minimum value described by the equation [0.64 * (rate of withdrawal of the oligomeric product from the reaction system)] -1.16 to the maximum value described by the equation [0.64 * (rate of withdrawal of the oligomeric product from the reaction system)] + 0.76. 4. Способ по п. 1, отличающийся тем, что соотношение объема теплообменной реакционной смеси к общему объему реакционной смеси реакционной системы находится в диапазоне от 0,70 до 1,0.4. The method according to p. 1, characterized in that the ratio of the volume of the heat exchange reaction mixture to the total volume of the reaction mixture of the reaction system is in the range from 0.70 to 1.0. 5. Способ по п. 1, отличающийся тем, что реакционная система дополнительно содержит участок реакционной системы, не обменивающийся теплом, содержащий объем реакционной смеси, не обменивающийся теплом и общую площадь поверхности, не обменивающуюся теплом, которая не обеспечивает теплообмен между реакционной смесью и теплоносителем, и при этом средняя температура реакционной смеси внутри участка реакционной системы, не обменивающегося теплом не превышает 0,61% средней температуры реакционной смеси в теплообменном участке реакционной системы.5. The method according to p. 1, characterized in that the reaction system further comprises a portion of the reaction system that does not exchange heat, containing a volume of the reaction mixture that does not exchange heat and a total surface area that does not exchange heat, which does not provide heat exchange between the reaction mixture and the coolant and the average temperature of the reaction mixture inside the portion of the reaction system that does not exchange heat does not exceed 0.61% of the average temperature of the reaction mixture in the heat exchange section of the reaction system we. 6. Способ по п. 1, отличающийся тем, что реакционная система дополнительно содержит участок реакционной системы, не обменивающийся теплом, содержащий объем реакционной смеси, не обменивающийся теплом и общую площадь поверхности, не обменивающуюся теплом, которая не обеспечивает теплообмен между реакционной смесью и теплоносителем, и при этом средняя температура теплообменной среды не превышает 9,3% средней температуры реакционной смеси в теплообменном участке реакционной системы.6. The method according to p. 1, characterized in that the reaction system further comprises a portion of the reaction system that does not exchange heat, containing a volume of the reaction mixture that does not exchange heat and a total surface area that does not exchange heat, which does not provide heat exchange between the reaction mixture and the coolant and the average temperature of the heat transfer medium does not exceed 9.3% of the average temperature of the reaction mixture in the heat exchange section of the reaction system. 7. Способ по п. 1, отличающийся тем, что реакционная система содержит реактор, выбранный из группы, состоящей из реактора непрерывного действия с механическим перемешиванием (CSTR), реактора идеального вытеснения или любых их комбинаций.7. The method according to p. 1, characterized in that the reaction system comprises a reactor selected from the group consisting of a continuous reactor with mechanical stirring (CSTR), a perfect displacement reactor, or any combination thereof. 8. Способ по п. 7, отличающийся тем, что реакционная система содержит реактор непрерывного действия с механическим перемешиванием, и при этом теплоноситель косвенно приведен в контакт с реакционной смесью внутри рубашки, вокруг по меньшей мере части внешней стенки реактора непрерывного действия с механическим перемешиванием, внутри внутренних спиралей теплообменников, или любых их комбинаций.8. The method according to p. 7, characterized in that the reaction system comprises a continuous reactor with mechanical stirring, and the coolant is indirectly brought into contact with the reaction mixture inside the jacket, around at least part of the outer wall of the continuous reactor with mechanical stirring, inside the internal coils of heat exchangers, or any combination thereof. 9. Способ по п. 7, отличающийся тем, что реакционная система содержит один или более реакторов идеального вытеснения, и при этом теплоноситель косвенно контактирует с реакционной смесью через стенку по меньшей мере одного участка по меньшей мере одного реактора идеального вытеснения.9. The method according to p. 7, characterized in that the reaction system contains one or more ideal displacement reactors, while the coolant indirectly contacts the reaction mixture through the wall of at least one section of at least one ideal displacement reactor. 10. Способ по п. 7, отличающийся тем, что реакционная система содержит путь реакционной смеси, включающий реактор, и при этом реакционную смесь рециркулируют через реактор, а соотношение объемной скорости потока рециркуляции реакционной смеси к объемной скорости выходного потока реакционной системы находится между 8 и 60.10. The method according to p. 7, characterized in that the reaction system comprises a reaction mixture path comprising a reactor, wherein the reaction mixture is recycled through the reactor, and the ratio of the volumetric rate of the recycle stream of the reaction mixture to the volumetric rate of the output stream of the reaction system is between 8 and 60. 11. Способ по п. 1, отличающийся тем, что олефиновый мономер состоит по существу из этилена.11. The method according to p. 1, characterized in that the olefin monomer consists essentially of ethylene. 12. Способ по п. 11, отличающийся тем, что каталитическая система содержит хром, гетероатомный лиганд и алкилметалл.12. The method according to p. 11, characterized in that the catalytic system contains chromium, a heteroatomic ligand and an alkyl metal. 13. Способ по п. 11, отличающийся тем, что каталитическая система содержит металлоорганическое соединение, состоящее по существу из триалкилалюминия.13. The method according to p. 11, characterized in that the catalytic system contains an organometallic compound consisting essentially of trialkylaluminum. 14. Способ по п. 11, отличающийся тем, что реакционная смесь содержит каталитическую систему, содержащую а) соединение никеля и бидентатный органофосфорин, содержащий по меньшей мере одну третичную фосфорорганическую группу или b) комплекс никеля и бидентатного органофосфорина, содержащего по меньшей мере одну третичную фосфорорганическую группу.14. The method according to p. 11, characterized in that the reaction mixture contains a catalytic system containing a) a nickel compound and a bidentate organophosphorine containing at least one tertiary organophosphorus group or b) a complex of nickel and a bidentate organophosphorine containing at least one tertiary organophosphorus group. 15. Способ по п. 11, отличающийся тем, что реакционная смесь содержит каталитическую систему, содержащую а) галогенид, гидрокарбилоксид или карбоксилат циркония, и алкилметалл, или b) галогенид, алкоксид или карбоксилат циркония, основание Льюиса и алкилметалл.15. The method according to p. 11, characterized in that the reaction mixture contains a catalytic system containing a) a zirconium halide, hydrocarbyl oxide or carboxylate, and alkyl metal, or b) zirconium halide, alkoxide or carboxylate, Lewis base and alkyl metal. 16. Способ по п. 11, отличающийся тем, что реакционная смесь содержит каталитическую систему, содержащую:16. The method according to p. 11, characterized in that the reaction mixture contains a catalytic system containing: a) комплекс переходного металла, включающий комплекс переходного металла с α-диимином и алкилметаллом,a) a transition metal complex comprising a transition metal complex with α-diimine and an alkyl metal, b) комплекс переходного металла, включающий комплекс переходного металла с пиридин 2,6-бисимином и алкилметаллом,b) a transition metal complex comprising a transition metal complex with pyridine 2,6-bisimine and an alkyl metal, c) соединение переходного металла, пиридин-2,6-бисимин и алкилметалл, илиc) a transition metal compound, pyridin-2,6-bisimine and an alkyl metal, or d) любую их комбинацию.d) any combination thereof. 17. Реакционная система для олигомеризации олефинового мономера, содержащая:17. A reaction system for oligomerizing an olefin monomer, comprising: один или более входов реакционной системы, выполненных с возможностью периодически или непрерывно вводить олефиновый мономер, каталитическую систему или компоненты каталитической системы, или любую их комбинацию в реакционную смесь реакционной системы;one or more inputs of the reaction system, configured to periodically or continuously introduce an olefin monomer, catalyst system or components of the catalyst system, or any combination thereof into the reaction mixture of the reaction system; один или более выходов реакционной системы, выполненных с возможностью периодически или непрерывно выводить выходящий поток реакционной системы, содержащий олигомерный продукт, из реакционной системы;one or more exits of the reaction system, configured to periodically or continuously withdraw the effluent of the reaction system containing the oligomeric product from the reaction system; общий объем реакционной смеси внутри реакционной системы; и the total volume of the reaction mixture within the reaction system; and теплообменный участок реакционной системы, содержащий объем теплообменной реакционной смеси и общую площадь поверхности теплообмена, обеспечивающую непрямой термоконтакт между реакционной смесью и теплоносителем;a heat exchange portion of the reaction system comprising a volume of a heat exchange reaction mixture and a total heat exchange surface area providing indirect thermal contact between the reaction mixture and the heat transfer medium; причем соотношение общей площади теплообменной поверхности к общему объему реакционной смеси реакционной системы находится в диапазоне от 0,75 дюйм-1 до 5 дюйм-1, иmoreover, the ratio of the total area of the heat exchange surface to the total volume of the reaction mixture of the reaction system is in the range from 0.75 inch -1 to 5 inch -1 , and при этом скорость вывода олигомерного продукта из реакционной системы составляет между от 1,0 фунт/час/галлон до 6,0 фунт/час/галлон.wherein the rate of withdrawal of the oligomeric product from the reaction system is between 1.0 lb / hr / gallon and 6.0 lb / hr / gallon. 18. Реакционная система по п. 17, отличающаяся тем, что соотношение общей площади теплообменной поверхности реакционной системы к общему объему реакционной смеси реакционной системы находится в диапазоне от минимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)]-1,16 до максимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)] + 0,76.18. The reaction system according to claim 17, characterized in that the ratio of the total heat exchange surface area of the reaction system to the total volume of the reaction mixture of the reaction system is in the range from the minimum value described by the equation [0.64 * (oligomer product withdrawal rate from the reaction system) ] -1.16 to the maximum value described by the equation [0.64 * (rate of withdrawal of the oligomeric product from the reaction system)] + 0.76. 19. Реакционная система по п. 17, отличающаяся тем, что соотношение объема теплообменной реакционной смеси к общему объему реакционной смеси реакционной системы находится в диапазоне от 0,70 до 1,0.19. The reaction system according to claim 17, characterized in that the ratio of the volume of the heat exchange reaction mixture to the total volume of the reaction mixture of the reaction system is in the range from 0.70 to 1.0. 20. Реакционная система по п. 17, отличающаяся тем, что реакционная система дополнительно содержит участок реакционной системы, не обменивающийся теплом, содержащий объем реакционной смеси, не обменивающийся теплом, и общую площадь поверхности, не обменивающуюся теплом, которая не обеспечивает теплообмен между реакционной смесью и теплоносителем, причем средняя температура реакционной смеси на участке реакционной системы, не обменивающимся теплом, не превышает 0,61% средней температуры реакционной смеси на теплообменном участке реакционной системы.20. The reaction system according to claim 17, characterized in that the reaction system further comprises a portion of the reaction system that does not exchange heat, containing a volume of the reaction mixture that does not exchange heat, and a total surface area that does not exchange heat, which does not provide heat exchange between the reaction mixture and coolant, and the average temperature of the reaction mixture in the portion of the reaction system that does not exchange heat does not exceed 0.61% of the average temperature of the reaction mixture in the heat exchange portion of the reaction oh system. 21. Реакционная система по п. 17, отличающаяся тем, что реакционная система дополнительно содержит участок реакционной системы, не обменивающийся теплом, содержащий объем реакционной смеси, не обменивающийся теплом, и общую площадь поверхности, не обменивающуюся теплом, которая не обеспечивает теплообмен между реакционной смесью и теплоносителем, причем средняя температура теплообменной среды не превышает 9,3% средней температуры реакционной смеси на теплообменном участке реакционной системы.21. The reaction system according to claim 17, characterized in that the reaction system further comprises a portion of the reaction system that does not exchange heat, containing a volume of the reaction mixture that does not exchange heat, and a total surface area that does not exchange heat, which does not provide heat exchange between the reaction mixture and a coolant, the average temperature of the heat exchange medium not exceeding 9.3% of the average temperature of the reaction mixture in the heat exchange section of the reaction system. 22. Реакционная система по п. 17, отличающаяся тем, что реакционная система содержит реактор, выбранный из группы, состоящей из реактора непрерывного действия с механическим перемешиванием (CSTR), реактора идеального вытеснения или любой их комбинации.22. The reaction system according to claim 17, wherein the reaction system comprises a reactor selected from the group consisting of a continuous mechanical stirring reactor (CSTR), a perfect displacement reactor, or any combination thereof. 23. Реакционная система по п. 22, отличающаяся тем, что реакционная система содержит один или более реакторов идеального вытеснения, и при этом теплоноситель косвенно приводят в контакт с реакционной смесью через стенку по меньшей мере участка по меньшей мере одного реактора идеального вытеснения.23. The reaction system according to claim 22, wherein the reaction system comprises one or more ideal displacement reactors, and the coolant is indirectly contacted with the reaction mixture through the wall of at least one section of the ideal displacement reactor. 24. Способ, включающий:24. A method comprising: периодическое или непрерывное введение олефинового мономера, и периодическое или непрерывное введение каталитической системы или компонентов каталитической системы в реакционную смесь реакционной системы, причем реакционная система содержит общий объем реакционной смеси реакционной системы; теплообменный участок реакционной системы, содержащий объем теплообменной реакционной смеси и общую площадь поверхности теплообмена, обеспечивающую непрямой термоконтакт между реакционной смесью и теплоносителем; олигомеризацию олефинового мономера в реакционной смеси с образованием олигомерного продукта;periodically or continuously introducing the olefin monomer, and periodically or continuously introducing the catalyst system or components of the catalyst system into the reaction mixture of the reaction system, the reaction system containing the total volume of the reaction mixture of the reaction system; a heat exchange portion of the reaction system comprising a volume of a heat exchange reaction mixture and a total heat exchange surface area providing indirect thermal contact between the reaction mixture and the heat transfer medium; oligomerizing the olefin monomer in the reaction mixture to form an oligomeric product; определение одного или более рабочих параметров реакционной системы во время олигомеризации;determining one or more operating parameters of the reaction system during oligomerization; управление одним или более рабочими параметрами реакционной системы во время олигомеризации; иcontrol of one or more operating parameters of the reaction system during oligomerization; and поддержание соотношения общей площади поверхности теплообмена к общему объему реакционной смеси реакционной системы в диапазоне от 0,75 дюйм-1 до 5 дюйм-1 управлением одним или более рабочими параметрами реакционной системы;maintaining the ratio of the total heat exchange surface area to the total volume of the reaction mixture of the reaction system in the range from 0.75 inch -1 to 5 inch -1 control of one or more operating parameters of the reaction system; периодический или непрерывный выпуск выходного потока реакционной системы, содержащий олигомерный продукт, из реакционной системы.periodically or continuously discharging the output of the reaction system containing the oligomeric product from the reaction system. 25. Способ по п. 24, дополнительно включающий поддержание скорости вывода олигомерного продукта из реакционной системы между 1.0 (фунт)(час-1)(галлон-1) и 6.0 (фунт)(час-1)(галлон-1) управлением одним или более рабочими параметрами реакционной системы.25. The method according to p. 24, further comprising maintaining the speed of output of the oligomeric product from the reaction system between 1.0 (pound) (hour -1 ) (gallon -1 ) and 6.0 (pound) (hour -1 ) (gallon -1 ) control one or more operating parameters of the reaction system. 26. Способ по п. 25, отличающийся тем, что один или более рабочих параметров реакционной системы включают объемную скорость входящего потока и объемную скорость выходящего потока реакционной системы, и при этом поддержание соотношения общей площади поверхности теплообмена к общему объему реакционной смеси реакционной системы управляется объемной скоростью входящего и объемной скоростью выходящего потоков реакционной системы.26. The method according to p. 25, characterized in that one or more operating parameters of the reaction system include the volumetric rate of the incoming stream and the volumetric rate of the output stream of the reaction system, while maintaining the ratio of the total heat exchange surface area to the total volume of the reaction mixture of the reaction system is controlled by volume the velocity of the incoming and the volumetric velocity of the outgoing streams of the reaction system. 27. Способ по п. 24, отличающийся тем, что один или более рабочих параметров реакционной системы включают концентрацию олигомерного продукта в реакционной смеси, и при этом поддержание скорости вывода олигомерного продукта контролируется концентрацией олигомерного продукта.27. The method according to p. 24, characterized in that one or more operating parameters of the reaction system include the concentration of the oligomeric product in the reaction mixture, while maintaining the speed of output of the oligomeric product is controlled by the concentration of the oligomeric product. 28. Способ по п. 24, дополнительно включающий поддержание соотношения общей площади теплообменной поверхности реакционной системы к общему объему реакционной смеси реакционной системы в диапазоне от минимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)]-1,16 до максимального значения, описанного уравнением [0,64* (скорость вывода олигомерного продукта из реакционной системы)] + 0,76 управлением одним или более рабочими параметрами реакционной системы.28. The method according to p. 24, further comprising maintaining the ratio of the total area of the heat exchange surface of the reaction system to the total volume of the reaction mixture of the reaction system in the range from the minimum value described by equation [0.64 * (rate of withdrawal of the oligomeric product from the reaction system)] - 1 , 16 to the maximum value described by the equation [0.64 * (rate of withdrawal of the oligomeric product from the reaction system)] + 0.76 by controlling one or more operating parameters of the reaction system. 29. Способ по п. 24, дополнительно включающий поддержание средней температуры реакционной смеси в участке реакционной системы, не обменивающимся теплом, в пределах 0,61% средней температуры реакционной смеси в теплообменном участке реакционной системы управлением одним или более рабочими параметрами реакционной системы.29. The method according to p. 24, further comprising maintaining the average temperature of the reaction mixture in the portion of the reaction system, not exchanging heat, within 0.61% of the average temperature of the reaction mixture in the heat exchange section of the reaction system by controlling one or more operating parameters of the reaction system. 30. Способ по п. 29, отличающийся тем, что один или более рабочих параметров реакционной системы включают среднюю температуру реакционной смеси внутри участка реакционной системы, не обменивающегося теплом, среднюю температуру реакционной смеси в пределах теплообменного участка реакционной системы, и среднюю температуру теплообменной среды, и при этом управление одним или более рабочими параметрами реакционной системы включает управление по меньшей мере средней температурой теплоносителя.30. The method according to p. 29, characterized in that one or more operating parameters of the reaction system include the average temperature of the reaction mixture inside the portion of the reaction system that does not exchange heat, the average temperature of the reaction mixture within the heat exchange portion of the reaction system, and the average temperature of the heat transfer medium, and wherein the control of one or more operating parameters of the reaction system includes controlling at least the average temperature of the coolant. 31. Способ по п. 30, дополнительно включающий поддержание средней температуры теплоносителя в пределах 9,3% средней температуры реакционной смеси в пределах теплообменного участка реакционной системы.31. The method according to p. 30, further comprising maintaining the average temperature of the coolant within 9.3% of the average temperature of the reaction mixture within the heat exchange section of the reaction system. 32. Способ по п. 24, дополнительно включающий поддержание значения числа Рейнольдса реакционной смеси внутри теплообменного участка реакционной системы между от 2×105 до 1×106 управлением одним или более рабочими параметрами реакционной системы.32. The method according to p. 24, further comprising maintaining the Reynolds number of the reaction mixture within the heat exchange portion of the reaction system between 2 × 10 5 to 1 × 10 6 controlling one or more operating parameters of the reaction system. 33. Способ по п. 32, отличающийся тем, что один или более рабочих параметров реакционной системы включают скорость потока реакционной смеси в теплообменном участке, рабочий параметр устройства для перемешивания или любую их комбинацию.33. The method according to p. 32, characterized in that one or more operating parameters of the reaction system include the flow rate of the reaction mixture in the heat exchange section, the operating parameter of the stirring device, or any combination thereof. 34. Способ по п. 24, дополнительно включающий рециркуляцию по меньшей мере части реакционной смеси реакционной системы; и поддержание соотношения объемной скорости вывода выходящего потока реакционной смеси для рециркуляции части реакционной смеси, рециклизованной в реакционную систему, к объемной скорости выходящего потока реакционной системы между 8 и 60.34. The method of claim 24, further comprising recirculating at least a portion of the reaction mixture of the reaction system; and maintaining the ratio of the volumetric rate of output of the effluent of the reaction mixture to recycle a portion of the reaction mixture recycled to the reaction system to the volumetric velocity of the effluent of the reaction system between 8 and 60.
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